US4566975A - Method for purifying aqueous solutions - Google Patents

Method for purifying aqueous solutions Download PDF

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Publication number
US4566975A
US4566975A US06/649,712 US64971284A US4566975A US 4566975 A US4566975 A US 4566975A US 64971284 A US64971284 A US 64971284A US 4566975 A US4566975 A US 4566975A
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stage
aqueous solution
precipitating
precipitate
precipitation
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US06/649,712
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English (en)
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Torkel Allgulin
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Boliden AB
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Boliden AB
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Assigned to BOLIDEN AKTIEBOLAG, A CORP. OF SWEDEN reassignment BOLIDEN AKTIEBOLAG, A CORP. OF SWEDEN ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: ALLGULIN, TORKEL
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/103—Arsenic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/906—Phosphorus containing
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/911—Cumulative poison
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/911—Cumulative poison
    • Y10S210/912—Heavy metal
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/911—Cumulative poison
    • Y10S210/912—Heavy metal
    • Y10S210/914—Mercury

Definitions

  • the present invention relates to a method for purifying aqueous solutions containing at least one impurity element from the group consisting of arsenic, phosphorus, mercury and other heavy metals and solid matter. More specifically, the invention relates to a method for removing impurities by precipitation in at least two stages in an acid-free environment with the aid of known precipitation reagents possessing ions capable of forming hydroxide precipitates.
  • arsenic can be isolated from aqueous solutions by precipitation with the aid of the system Me n+ /Me(OH) n , i.e. a combination of free ions and hydroxide of the element Me.
  • Me n+ /Me(OH) n i.e. a combination of free ions and hydroxide of the element Me.
  • Mn, Zn, Cd, Cr, Fe, Al and Ca Of these elements, Fe, Al and Ca are considered the most suitable for use in the present context, since they do not create environmental problems of an unduly serious nature.
  • the precipitation reagent When separating the impurities by precipitation in accordance with known methods, however, the precipitation reagent must be used in a quantity which ensures a substantial stoichiometric excess of precipitation-ions.
  • the reason herefor is thought to be because a percentage of the precipitation-ions introduced form complexes in the solution and thereby become inactive.
  • many of the ions in question e.g. Al and Fe, are liable to build complexes in aqueous solutions, in the presence of sulphur dioxide, to form sulphur/oxy-compounds.
  • phosphorous is precipitated from the aqueous solution with the aid of lime in a single stage, and part of the slime formed during this precipitation process is returned to the process, to be mixed with the precipitation reagent as it is charged to the aqueous solution.
  • the best reagents for use in this connection are iron and aluminium ions, although other metal ions, such as Mn, Zn, Cd and Cr, can also be used.
  • metal ions such as Mn, Zn, Cd and Cr
  • magnesium and/or calcium compounds it is also possible in certain instances to use magnesium and/or calcium compounds.
  • the hydroxide solubility of the metals in group 2a of the periodic system is high, they can still be used as a precipitation reagent in concentrated solutions containing large quantities of impurities.
  • the group 2a metals are highly attractive sources of hydroxide, and hence they can be used in spite of their aforementioned drawbacks.
  • the impurities in question are precipitated in two or more stages, in which a large percentage of the precipitation reagent is supplied in the second stage and also to any subsequent stage.
  • a hydroxide precipitate which contains the impurities and which can be substantially completely separated from the solution. No harm is caused if a minor part of the aqueous solution accompanies the precipitate when it is separated from the solution, provided that substantially all of the precipitate is removed from the remainder of the solution.
  • the aqueous solution from which the precipitate has been removed can be safely dumped, while the precipitate itself, together with any accompanying solution, can be returned to the water.
  • the procedure adopted when returning the precipitate can take many forms, the important thing being that the precipitate is present in the first precipitation stage.
  • the precipitate can be returned to the impure aqueous solution introduced to the first precipitation stage, optionally subsequent to alkalizing the precipitate if necessary, or alternatively, if found more practical, the precipitate can be returned directly to the first precipitation stage.
  • the precipitate may first be dissolved in water before being returned to the aqueous solution before or in the first precipitation stage.
  • the precipitate present in the aqueous solution subsequent to the first precipitation stage is removed from said stage in the form of a mud or sludge, prior to introducing the aqueous solution to the second precipitation stage.
  • the quantity of precipitation agent supplied to the various stages is adapted so that the ratio of the amount of precipitation ions present in the solution to the amount of impurity element ions contained therein is much lower than in subsequent stages. More specifically, it should be ensured that the quantity of precipitation reagent supplied to the first stage is such that the ratio of equivalents of precipitation metal-ions to moles of impurity elements is at least 0.8, preferably between 1 and 3, said ratio being expressed hereinafter as X. In the last stage the ratio X is suitably at least 2, preferably between 10 and 15.
  • the precipitation reagent introduced can be divided between the second stage and any subsequent stage or stages, although it is preferably introduced to the last stage, so as to obtain the aforementioned ratio X in the final stage of the process.
  • the solution should be alkaline or should at least have a pH at which hydroxide precipitations are formed. Consequently, it may be necessary to add alkali, suitably Ca(OH) 2 , NaOH or NH 4 OH, prior to the first precipitation stage. In this respect, it has been found advantageous to maintain a pH in the solution of at least about 9 when precipitating Me(OH) 2 -impurity element in the first stage. In the second stage, or any subsequent stage, a pH of between 8 and 9 is sufficient to achieve acceptable precipitation. The pH can be lower when using other hydroxide builders, such as Me 3+ -ions.
  • Sludge present in the solution subsequent to the first stage is suitably separated from said solution mechanically, preferably by centrifugation, there being obtained in this way an extremely thick sludge. It is not absolutely necessary for all of the sludge to be removed at this stage, since any remaining sludge will be isolated and removed after the final stage, and returned to the process.
  • Precipitation is best carried out at solution temperatures beneath about 50° C., and preferably beneath 30° C.
  • FIGURE is a flow sheet illustrating a preferred embodiment of the invention, and also with reference to a number of practical working examples.
  • a contaminated solution is charged to a mixing tank 10, to which alkali and optionally also return sludge are also charged.
  • Alkali is charged to the tank 10, to adjust the pH of the solution to about 9.0.
  • the thus alkalised solution is pumped through a pipe 11 to a first precipitation tank 12.
  • FeSO 4 is added to the solution in the tank 12, to which sludge containing impurities and iron separated from a subsequent precipitation stage, is also charged through a pipe 13.
  • Iron sulphate is added solely in an amount which provides a total ratio X of at least 1-3. In this way, between 70 and 80% of the impurity content of the solution is precipitated out.
  • Solution and precipitate are removed from the tank 12 through a pipe 14, and passed to a separation plant 15, which suitably comprises a separator. At least a substantial part of the precipitate present is separated from the solution in the separator 15. As previously indicated, it is not necessary to attempt to remove all the precipitate at this stage.
  • the impurity-containing sludge separated from the solution is removed for further processing with respect to its content of impurity and precipitating agent metals.
  • the solution freed from the major part of its impurity content in the separator 15 is then pumped to a further precipitation tank 17.
  • Alkali here exemplified as NaOH
  • a precipitation agent here exemplified as FeSO 4 .
  • the amount of alkali added to the solution is adapted so that, subsequent to adding FeSO 4 , the pH of said solution lies within the range of 8.0-9.0, while the amount of sulphate added is adapted so that the ratio X in the solution lies between 10 and 15. In this way, impurity elements can be precipitated-out to a residual content of less than 1 mg/l solution.
  • the majority of the precipitate formed often comprises a relatively voluminous iron-hydroxide with impurity ions such as AsO 2 - adsorbed thereon. Any mercury and other heavy metals present in the solution will thus be precipitated out, together with any arsenic and phosphorous and the iron, to leave extremely low residual contents.
  • iron sulphate as the precipitation agent, it has, for example, been found possible to precipitate mercury to residual contents beneath about 10 -3 mg/l, as compared with the relatively high residual contents of from 10 -1 -10 -3 mg/l achievable with hitherto known methods.
  • the solution and the precipitate present therein is passed through a pipe 18 to a flocculating tank 20, to which a suitable flocculating agent is passed through a supply pipe 19.
  • the thus treated solution is pumped from the flocculating tank 20 through a pipe 21 to a lamella separator 22.
  • the flocculated precipitate is separated from the solution in the lamella separator, and is removed in the form of a sludge from the bottom of the separator 22, as indicated by the line 23, while cleansed solution is removed via an overflow pipe 24, and passed to a cloth filter 25, where the solution is cleansed still further and from which the filtered, purified solution is withdrawn and dumped.
  • the sludge taken from the bottom of the lamella separator 22 is passed through the pipe 23 and the pipe 13 back to the first precipitation tank 12, or through the pipe 13 A shown in broken lines and back to the mixing tank 10.
  • the sludge can be charged to the ingoing solution and mixed therewith, prior to charging the solution to the mixing tank 10.
  • Those impurity-element containing aqueous solutions which can be advantageously purified by means of the method according to the invention include acid condensate containing arsenic, mercury, selenium, cadmium and any other heavy metals and any solid matter formed when cooling roaster gases in accordance with the roaster-gas cleansing method described in U.S. Pat. No. 4,138,231 assigned to Boliden Aktiebolag.
  • the invention can advantageously be generally employed for the purification of process water solutions derived from chemical and metallurgical industries, especially solutions containing arsenic and heavy metals.
  • the condensate had a pH of 0.5-1.5.
  • the pH was adjusted to about 9 by adding 25% NaOH.
  • Oxidic iron-arsenic sludge was charged to step 1 and FeSO 4 was charged to stage 2.
  • the FeSO 4 charged to stage 2 was in the form of a non-acid solution having a pH of 8-9.
  • the iron was charged in an amount such that the weight ratio Fe/As in the first stage was about 0.5 and in the second stage about 7.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Removal Of Specific Substances (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Detergent Compositions (AREA)
  • Treatment Of Sludge (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
US06/649,712 1983-09-12 1984-09-12 Method for purifying aqueous solutions Expired - Lifetime US4566975A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8304858A SE452307B (sv) 1983-09-12 1983-09-12 Forfarande for rening av fororenade vattenlosningar innehallande arsenik och/eller fosfor
SE8304858 1983-09-12

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US4566975A true US4566975A (en) 1986-01-28

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US (1) US4566975A (el)
EP (1) EP0139622B1 (el)
JP (1) JPS60143893A (el)
AT (1) ATE31289T1 (el)
BR (1) BR8404502A (el)
CA (1) CA1253981A (el)
DE (1) DE3468010D1 (el)
ES (1) ES535544A0 (el)
GR (1) GR80306B (el)
MA (1) MA20224A1 (el)
MX (1) MX7707E (el)
PT (1) PT79186B (el)
SE (1) SE452307B (el)
YU (1) YU43855B (el)
ZA (1) ZA846790B (el)

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US4717484A (en) * 1985-03-06 1988-01-05 Kaeuffer Karl C Process for completing circulatory systems used to purify water and sewage
WO1988010243A1 (en) * 1987-06-18 1988-12-29 Bethlehem Steel Corporation Process for chemical stabilization of heavy metal bearing dusts and sludges, such as eaf dust
US4814091A (en) * 1987-06-29 1989-03-21 The United States Of America As Represented By The United States Department Of Energy Process for removing metals from water
US4840671A (en) * 1987-06-18 1989-06-20 Bethlehem Steel Corporation Process for chemical stabilization of heavy metal bearing dusts and sludges as EAF dust
EP0364423A1 (en) * 1988-10-11 1990-04-18 Boliden Contech Ab A method for purifying contaminated aqueous solutions
US4940549A (en) * 1989-01-31 1990-07-10 Santina Water Company Method for removing toxic metals from agricultural drain water
US5039428A (en) * 1990-03-05 1991-08-13 Tetra Technologies, Inc. Waste water treatment process using improved recycle of high density sludge
US5093007A (en) * 1989-05-24 1992-03-03 Nerco Minerals Company Process for removal of inorganic and cyanide contaminants from wastewater
US5114592A (en) * 1989-03-31 1992-05-19 Walhalla-Kalk, Entwichlungs- Und Vertriebsgesellschaft Mbh Procedure for separating arsenic from waste material
US5128047A (en) * 1990-04-20 1992-07-07 Rhone-Poulenc Inc. Sequential separation of metals by controlled pH precipitation
US5200087A (en) * 1990-12-12 1993-04-06 Kubota Corporation Method of and apparatus for recovering mercury from drainage
US5200082A (en) * 1991-07-02 1993-04-06 Santina Water Company Method for removing toxic substances from industrial and agricultural waste water
US5252003A (en) * 1990-10-29 1993-10-12 International Technology Corporation Attenuation of arsenic leaching from particulate material
US5259697A (en) * 1987-06-18 1993-11-09 Bethlehem Steel Corporation Composition and process for forming low permeability barriers for waste disposal sites
US5262063A (en) * 1992-05-14 1993-11-16 Elf Atochem North America, Inc. Multiple-stage precipitation process for heavy metals in aqueous solution
US5348662A (en) * 1992-05-14 1994-09-20 Elf Atochem North America, Inc. Process for removing heavy metals from aqueous solutions
US5368703A (en) * 1992-05-12 1994-11-29 Anco Environmental Processes, Inc. Method for arsenic removal from wastewater
US5443622A (en) * 1994-02-28 1995-08-22 Kennecott Corporation Hydrometallurgical processing of impurity streams generated during the pyrometallurgy of copper
US5543049A (en) * 1991-02-04 1996-08-06 Delman R. Hogen Microbial mediated water treatment
US5545331A (en) * 1991-04-08 1996-08-13 Romar Technologies, Inc. Recycle process for removing dissolved heavy metals from water with iron particles
US5616168A (en) * 1994-02-28 1997-04-01 Kennecott Utah Copper Corporation Hydrometallurgical processing of impurity streams generated during the pyrometallurgy of copper
US5618439A (en) * 1993-04-20 1997-04-08 Boliden Contech Ab Method for purifying industrial sewage water
US5620893A (en) * 1992-07-16 1997-04-15 Delman R. Hogen Microbial mediated method for soil and water treatment
US5720882A (en) * 1993-08-26 1998-02-24 Kemira Kemi Ab Treatment method for waste water sludge comprising phoshorous, heavy metals and at least one metal
US5728295A (en) * 1996-04-19 1998-03-17 Fuji Hunt Photographic Chemicals, Inc. Apparatus for removing metal ions and/or complexes containing metal ions from a solution
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US20080093580A1 (en) * 2003-01-29 2008-04-24 Union Oil Company Of California Dba Unocal Composition for removing arsenic from aqueous streams
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US20100187178A1 (en) * 2003-01-29 2010-07-29 Molycorp Minerals, Llc Process for removing and sequestering contaminants from aqueous streams
US20100230359A1 (en) * 2009-03-16 2010-09-16 Molycorp Minerals, Llc Porous and durable ceramic filter monolith coated with a rare earth for removing contaminants from water
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US20100258448A1 (en) * 2009-04-09 2010-10-14 Molycorp Minerals, Llc Use of a rare earth for the removal of antimony and bismuth
US20110110817A1 (en) * 2009-11-09 2011-05-12 Molycorp Minerals, Llc Rare earth removal of colorants
US20110220577A1 (en) * 2010-03-12 2011-09-15 Council Of Scientific & Industrial Research Process for the removal of arsenic and chromium from water
US20110296949A1 (en) * 2010-06-08 2011-12-08 C.V.G. Ferrominera Orinoco C.A. Process and equipment for the production of direct reduced iron and/or pig iron from iron ores having a high-phosphorus content
US8349764B2 (en) 2007-10-31 2013-01-08 Molycorp Minerals, Llc Composition for treating a fluid
US9233863B2 (en) 2011-04-13 2016-01-12 Molycorp Minerals, Llc Rare earth removal of hydrated and hydroxyl species
US9975787B2 (en) 2014-03-07 2018-05-22 Secure Natural Resources Llc Removal of arsenic from aqueous streams with cerium (IV) oxide compositions

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US4724084A (en) * 1986-03-28 1988-02-09 The Boeing Company System for removing toxic organics and metals from manufacturing wastewater
DE3633066C2 (de) * 1986-09-29 1993-12-02 Fraunhofer Ges Forschung Verfahren zum Entfernen von Arsen aus Prozeßwässern der Glasindustrie
DE3908491A1 (de) * 1989-03-15 1990-09-20 Fraunhofer Ges Forschung Verfahren zur entfernung von arsen und/oder antimon aus loesungen, die arsen und/oder antimon als anionische fluorokomplexe enthalten

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ZA846790B (en) 1985-04-24
JPH0521637B2 (el) 1993-03-25
PT79186B (en) 1986-08-14
SE8304858D0 (sv) 1983-09-12
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ATE31289T1 (de) 1987-12-15
GR80306B (en) 1985-01-08
YU43855B (en) 1989-12-31
MX7707E (es) 1990-09-25
EP0139622A1 (en) 1985-05-02
ES8603355A1 (es) 1985-12-16
ES535544A0 (es) 1985-12-16
DE3468010D1 (en) 1988-01-21
SE8304858L (sv) 1985-03-13
YU156984A (en) 1987-06-30
PT79186A (en) 1984-10-01
CA1253981A (en) 1989-05-09
JPS60143893A (ja) 1985-07-30
SE452307B (sv) 1987-11-23
MA20224A1 (fr) 1985-04-01
BR8404502A (pt) 1985-08-06

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